CN200980986Y - Circulation fluidized bed dry method smoke desulphurizing device - Google Patents
Circulation fluidized bed dry method smoke desulphurizing device Download PDFInfo
- Publication number
- CN200980986Y CN200980986Y CN 200620048392 CN200620048392U CN200980986Y CN 200980986 Y CN200980986 Y CN 200980986Y CN 200620048392 CN200620048392 CN 200620048392 CN 200620048392 U CN200620048392 U CN 200620048392U CN 200980986 Y CN200980986 Y CN 200980986Y
- Authority
- CN
- China
- Prior art keywords
- flue gas
- reaction tower
- agitator
- desulfurization
- desulfurization reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- 238000000034 method Methods 0.000 title claims description 16
- 239000000779 smoke Substances 0.000 title description 2
- 238000006243 chemical reaction Methods 0.000 claims abstract description 51
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 41
- 239000003546 flue gas Substances 0.000 claims abstract description 40
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 39
- 230000023556 desulfurization Effects 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000003756 stirring Methods 0.000 claims description 25
- 238000012216 screening Methods 0.000 claims description 17
- 230000003009 desulfurizing effect Effects 0.000 claims description 13
- 239000003795 chemical substances by application Substances 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 11
- 230000005540 biological transmission Effects 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 10
- 238000005243 fluidization Methods 0.000 abstract description 5
- 239000000203 mixture Substances 0.000 abstract description 5
- 230000007797 corrosion Effects 0.000 abstract description 3
- 238000005260 corrosion Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000001035 drying Methods 0.000 abstract 1
- 238000005194 fractionation Methods 0.000 abstract 1
- 239000011440 grout Substances 0.000 abstract 1
- 239000000463 material Substances 0.000 description 29
- 239000007787 solid Substances 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 5
- 238000006062 fragmentation reaction Methods 0.000 description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 4
- 239000000920 calcium hydroxide Substances 0.000 description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 4
- 238000013467 fragmentation Methods 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000001079 digestive effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000001483 mobilizing effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000012257 stirred material Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a flue gas desulfurization unit employing circulating fluid-bed drying, characterized in that an agitator consisting of a barrel, a rotating agitating device, a desulfurizer inlet, a fluidization air inlet, a water inlet and a fractionation air duct is arranged at the bottom portion of a desulfurization reaction tower and is capable of agitating, fragmenting and fluidifying, screen selecting, and feeding, and a flue gas inlet is arranged on the passageway between the desulfuration reaction tower and a Venturi tube. With the employment of the utility model, the flue gas first go down to the bottom of the desulfurization reaction tower after entering the passageway of the desulfurization reaction tower, carrying the mixture flowing out of the agitator to turn up through the Venturi tube at a low velocity into the desulfurization reaction main tower, and the flow velocity of the turning up and going through of the flue gas is very low, further, after being fragmented by the agitator and fluidified, screen selected, and fed, grout containing bulky grain is not contained in the desulfurization reaction tower, the grain diameter of particles in the mixture is small, the moisture percentage of the particles is high, and the activity of the particles is high, the availability ratio of the desulfurizer is high, avoiding scale formation and corrosion, and in the desulfurization reaction tower the flow velocity of the flue gas is low and the resistance against the flue gas is small, the intensity of heat transfer and mass transfer is high, the efficiency of the desulfurization is high, and the energy consumption of the desulfurization is small.
Description
Technical field
The utility model relates to a kind of flue gas desulfur device, relates in particular to a kind of circulation fluidized bed dry method flue gas desulfur device, is used for removing sulfur oxide and other harmful sour gas of the flue gas of being discharged by boiler or other combustion apparatus, as HCL, and HF etc.
Background technology
In common circulation fluidized bed dry method flue gas desulfur technology, as CFB-FGD and RCFB-FGD technology, calcium hydroxide and water are injected in the desulfurizing tower and flue gas mixes, flue-gas temperature drops to 15～25 ℃ near dew-point temperature, be generally 65～75 ℃, wish that sulfur in smoke and other sour gas produce the ionic reaction of gas-liquid, liquid-solid high speed with moistening calcium hydroxide, but because the average moisture content of calcium hydroxide and recycle stock is very low, only be about 1%, gas-solid reaction can only occur in the surface of solids, and reaction speed is very slow.(number of patent application: 00128285.9) " a kind of dry cyclic suspension bed fume desulfurizing process and system thereof " technology all directly adds water to lime and recycle stock and stirs for the NID that addresses this problem ABB AB and Chinese invention patent application, make it form water capacity at 5%～15% mixed material, but owing to there is not screening plant, the particle of mixed material and cluster of grains average grain diameter enlarge markedly along with the increase of water capacity, this causes the specific area of mixed material to descend on the one hand, the active reduction, need set out cinder notch in the bottom of desulfurization reaction tower on the other hand, the desulfurizing agent short circuit of the not complete reaction of a large amount of conglomerations is directly got rid of from slag notch, causes the waste of desulfurizing agent.Above-mentioned in addition various technology reduce the sedimentation of bulky grain and cluster of grains in order to hold up mixed material, and the air velocity in the Venturi tube is 25～40 seconds/meter under rated loan condition, causes the flue gas resistance height of desulfurization reaction tower.
Summary of the invention
The purpose of this utility model is in order to overcome above-mentioned the deficiencies in the prior art, provide a kind of desulfurizing agent and recycle stock of making to carry out abundant stirring and screening with water, produce moisture content height, the thin mixed material of granularity, the flow velocity that flue gas flows through Venturi tube and desulfurization reaction tower is low, the circulation fluidized bed dry method flue gas desulfur device that flue gas resistance is low.
The purpose of this utility model is achieved by the following technical solution: a kind of circulation fluidized bed dry method flue gas desulfur device, and it comprises desulfurization reaction tower, agitator, material-returning device and deduster, is characterized in:
1. described agitator is arranged in the desulphurization reaction tower bottom; Agitator is made up of cylindrical shell, rotating stirring device, desulfurizing agent inlet, fluidized wind inlet, water inlet and screening air channel, rotating stirring device places in the cylindrical shell, fluidized wind inlet, water inlet place a side of cylindrical shell, are that the screening air channel of one is connected with the desulphurization reaction tower bottom with cylindrical shell;
2. described desulfurization reaction tower is by gas approach, passageway, Venturi tube, desulphurization reaction king-tower and be connected flue and form, and described gas approach places on the passageway that desulfurization reaction tower and Venturi tube form.
Rotating stirring device in the described agitator is that single axle rotation agitating device or twin shaft agitating device are formed, the twin shaft agitating device is placed in the same cylindrical shell by two single axle rotation agitating devices are parallel, and the centre is equipped with dividing plate and constitutes the first order, second level two-stage rotating stirring device.Described two-stage rotating stirring device structure is identical.Described single axle rotation agitating device comprises motor, rotating shaft, positive blade, anti-blade and scraper plate.
Because the utility model will have the bottom that the agitator that adds water stirring, fragmentation and fluidisation screening conveying function is arranged in desulfurization reaction tower, gas approach places on the passageway of desulfurization reaction tower and Venturi tube composition, its beneficial effect is after making flue gas enter the desulfurization reaction tower passageway, arrive its bottom earlier downwards, turning is carried the mixed material that the flows out agitator low speed that makes progress and is passed through Venturi tube, enter the desulphurization reaction king-tower, the turning of flue gas and all very low by the flow velocity of Venturi tube; Mixed material adds water stirring, fragmentation and fluidisation screening through agitator to be carried, and makes no oarse-grained slurries in desulfurization reaction tower, and the grain diameter of mixed material is thin, the moisture content height, active strong, the utilization rate height of desulfurizing agent, the desulfurization and dedusting process does not have the sorrow of fouling and corrosion; The good reliability of this device, desulfurization reaction tower flue gas flow rate lower resistance is little, heat and mass intensity height, the desulfuration efficiency high energy consumption is few.
Description of drawings
Fig. 1 is a kind of structural representation of circulation fluidized bed dry method flue gas desulfur device;
Fig. 2 is a single shaft agitator structure front view;
Fig. 3 is a single shaft agitator structure vertical view;
Fig. 4 is the A-A view of Fig. 3.
Fig. 5 is the double-shaft mixers structural front view;
The specific embodiment
Below in conjunction with accompanying drawing the utility model is elaborated:
Shown in Fig. 1-5, a kind of circulation fluidized bed dry method flue gas desulfur device, it comprises desulfurization reaction tower, agitator, material-returning device and deduster, is characterized in:
1. described agitator 15 is arranged in the desulphurization reaction tower bottom; Agitator 15 is made up of cylindrical shell 19, rotating stirring device, desulfurizing agent inlet 13, fluidized wind inlet 12, water inlet 14 and screening air channel 17, rotating stirring device places in the cylindrical shell 19, fluidized wind inlet 12, water inlet 14 place a side of cylindrical shell 19, are connected with the desulphurization reaction tower bottom for the screening air channel 17 of one with cylindrical shell 19;
2. described desulfurization reaction tower is by gas approach 1, passageway 2, Venturi tube 3, desulphurization reaction king-tower 5 and be connected flue 6 and form, and described gas approach 1 places on the passageway 2 that desulfurization reaction tower and Venturi tube form.
Deduster described in the utility model is a gas-solid separator 7, desulfurization reaction tower joins with gas-solid separator 7 by connecting flue 6, be furnished with ash bucket 8 in the bottom of gas-solid separator 7, strength skewed slot 9, the material-returning device that outlet 10 of desulfurization ash and rotary feeder 11 are formed, dirty flue gas enters desulfurization reaction tower from gas approach, with the mixed material hybrid reaction that flows out agitator after, sour gas is wherein effectively removed, enter gas-solid separator 7 again and remove most solid particles, finally, cleaning flue gases is discharged by the exhanst gas outlet 16 that is located on the separator, the ash that gas-solid separator 7 separates, major part enters agitator 15 as recycle stock by rotary feeder 11, and is remaining from desulfurization ash outlet 10 discharges.After flue gas enters the passageway 2 of desulfurization reaction tower and Venturi tube composition, downward its bottom that arrives of flue gas elder generation, the 180 ° of low speed that make progress of mixed material turning that carry outflow agitator 15 enter desulphurization reaction king-tower 5 by Venturi tube 3 shown in Fig. 1 flue gas flow direction 4; Recycle stock, desulfurizing agent and fluidized wind 20 enter agitator 15 by entering the mouth, and stir with water, and the mixed material of generation upwards flows out agitator 15 at scraper plate 23 and screening air channel 17, wind action lower edge.Rotating stirring device in the described agitator 15 is that single axle rotation agitating device or twin shaft agitating device are formed, the twin shaft agitating device is placed in the same cylindrical shell 19 by two single axle rotation agitating devices are parallel, and the centre is equipped with dividing plate 26 and constitutes the first order, second level two-stage rotating stirring device.Material enters second level agitating device by first order stirred materials through dividing plate 26 tops, and double-shaft mixers can make the more even of mixing of materials.
Described single axle rotation agitating device comprises motor 25, rotating shaft 18, positive blade 21, anti-blade 22 and scraper plate 23, described positive blade 21 anti-blades 22 are along uniform 4 or 6 groups altogether of circumference, blade and rotating shaft 18 axis form 45～70 ° angle, the angle and the shaft axis of positive and negative blade are symmetrical, scraper plate 23 is connected in the front end of blade, form one 45～90 ° angle with direction of rotation 24, the width of scraper plate 23 is 1/10～1/6 of cylindrical shell 19 diameters.The single axle rotation agitating device plays a part to stir and carry to mixed material, under the drive of motor 25, along with the rotation of rotating shaft 18 along direction of rotation 24, positive blade 21 moves upward, and anti-blade 22 moves downward, under the promotion of blade, one side material is when left movement, the opposite side material just moves right, and material is mixed fully, and scraper plate is delivered to the screening air channel with mixed material.The two-stage rotating stirring device structural similarity of double-shaft mixers, the transmission of two-stage rotating stirring device by one of them motor by linkage or connect motor separately and realize, the width of the scraper plate 27 of first order rotating stirring device is 1/20～1/10 of a barrel diameter, it is transported to second level agitating device with mixed material, by scraper plate 23 continuous at length direction or that interruption is arranged mixed material is transported to screening air channel 17.The length in screening air channel equates with the width of desulfurization reaction tower, width is 1/5～1/3 of a barrel diameter, the Dual-Phrase Distribution of Gas olid mean flow rate is 0.1～0.5 meter per second, sieve by strength, tiny particle flows out agitator, bulky grain and cluster of grains then sedimentation return in the cylindrical shell of agitator, are stirred the friction fragmentation repeatedly, until the outflow agitator that attenuates.This can improve the moisture content of mixed material to greatest extent under the prerequisite that guarantees grain fineness.Mixed material is under the acting in conjunction of blade, scraper plate and strength screening, can produce water content and be at least 5%, particle and cluster of grains average grain diameter are not more than 50 microns mixed material, by regulating injection flow rate, recycle stock amount and fluidisation air quantity, the weight moisture capacity of preferably controlling mixed material is 10%～20%, and particle and cluster of grains average grain diameter are not more than 30 microns.
Gas-solid separator 7 can be electrostatic precipitator or sack cleaner, also can be inertia or the cyclone dust collectors assembly with electrostatic precipitator or sack cleaner.
By the circulation repeatedly of material, in desulfurization reaction tower, the concentration of mixed material can be up to 1 kilogram/meter about 3, and along with agglomeration of particles, the cluster of grains that some concentration is high can be settled down at the bottom of the tower.The utility model is arranged in the desulphurization reaction tower bottom with agitator, just can send these particle humidification activation fragmentations back to king-tower, can not cause mixed material short circuit waste, so can choose low flue gas flow rate in desulfurization reaction tower, one reduces flue gas resistance; Two increase the interior circulation of material; Three come heat and mass transfer enhancement and chemical reaction.Usually under declared working condition, flue gas is turned and the flow velocity by Venturi tube is not more than 15 meter per seconds, and the flow velocity of flue gas in the desulphurization reaction king-tower is not more than 7 meter per seconds; Best is, and flue gas turns and the flow velocity by Venturi tube is no more than 12 meter per seconds, and the flow velocity of flue gas in the desulphurization reaction king-tower is not more than 5 meter per seconds.
In the utility model, agitator had both had the humidification by mixing of gas digestive function, also had certain broken mobilizing function, so desulfurizing agent promptly can be solid-state calcium-based desulfurizing agent, lime or calcium hydroxide also can be flying dust or other alkaline matters that contains alkaline matter.
Because the utility model is arranged in the bottom of desulfurization reaction tower with agitator, has the water of adding and stirs The function of mix, the screening of fragmentation and fluidisation being carried, its advantage is not have bulky grain in desulfurization reaction tower Slurries, the grain diameter of mixed material is thin, the moisture content height is active strong, the utilization of desulfurizing agent The rate height; The desulfurization and dedusting process does not have the sorrow of fouling and corrosion, the good reliability of device; Desulphurization reaction Tower flue gas flow velocity lower resistance is little, heat and mass intensity height, and the desulfuration efficiency high energy consumption is few.
Claims (5)
1. circulation fluidized bed dry method flue gas desulfur device, it comprises desulfurization reaction tower, agitator, material-returning device and deduster, it is characterized in that:
1) described agitator (15) is arranged in the desulphurization reaction tower bottom; Agitator (15) is made up of cylindrical shell (19), rotating stirring device, desulfurizing agent inlet (13), fluidized wind inlet (12), water inlet (14) and screening air channel (17), rotating stirring device places in the cylindrical shell (19), fluidized wind inlet (12), water inlet (14) place a side of cylindrical shell (19), are connected with the desulphurization reaction tower bottom for the screening air channel (17) of one with cylindrical shell (19);
2) described desulfurization reaction tower is by gas approach (1), passageway (2), Venturi tube (3), desulphurization reaction king-tower (5) be connected flue (6) and form, and described gas approach (1) places on the passageway (2) that desulfurization reaction tower and Venturi tube form.
2. circulation fluidized bed dry method flue gas desulfur device according to claim 1, it is characterized in that: the rotating stirring device in the described agitator (15) is that single axle rotation agitating device or twin shaft agitating device are formed, the twin shaft agitating device is placed in the same cylindrical shell (19) by two single axle rotation agitating devices are parallel, and the centre is equipped with the rotating stirring device that dividing plate (26) constitutes the first order, second level two-stage.
3. circulation fluidized bed dry method flue gas desulfur device according to claim 2, it is characterized in that, described single axle rotation agitating device comprises motor (25), rotating shaft (18), positive blade (21), anti-blade (22) and scraper plate (23), the anti-blade of described positive blade (21) (22) is along uniform 4 or 6 groups altogether of circumference, blade and rotating shaft (18) axis forms 45～70 ° angle, the angle and the shaft axis of positive and negative blade are symmetrical, scraper plate (23) is connected in the front end of blade, form one 45～90 ° angle with direction of rotation (24), the width of scraper plate (23) is 1/10～1/6 of cylindrical shell (a 19) diameter.
4. circulation fluidized bed dry method flue gas desulfur device according to claim 2, it is characterized in that, the transmission of described two-stage rotating stirring device by one of them motor by linkage or connect motor separately and realize that the width of the scraper plate of first order rotating stirring device (27) is 1/20～1/10 of a barrel diameter.
5. circulation fluidized bed dry method flue gas desulfur device according to claim 1 is characterized in that, the width in described screening air channel (17) is 1/5～1/3 of a barrel diameter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620048392 CN200980986Y (en) | 2006-12-01 | 2006-12-01 | Circulation fluidized bed dry method smoke desulphurizing device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620048392 CN200980986Y (en) | 2006-12-01 | 2006-12-01 | Circulation fluidized bed dry method smoke desulphurizing device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN200980986Y true CN200980986Y (en) | 2007-11-28 |
Family
ID=38908150
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200620048392 Expired - Lifetime CN200980986Y (en) | 2006-12-01 | 2006-12-01 | Circulation fluidized bed dry method smoke desulphurizing device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN200980986Y (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100460047C (en) * | 2006-12-01 | 2009-02-11 | 沙晓农 | Circulation fluidized bed dry method flue gas desulfur device |
| CN102266718A (en) * | 2010-06-07 | 2011-12-07 | 中国科学院过程工程研究所 | Semi dry process flue gas desulfurization method of circulating fluidized bed based on circulation, and apparatus thereof |
| CN102397729A (en) * | 2011-12-12 | 2012-04-04 | 中联重科股份有限公司 | Dust removal case and have dust pelletizing system of this dust removal case |
| CN107570000A (en) * | 2017-10-31 | 2018-01-12 | 苏州顺为环境科技有限公司 | Deacidifying dedusting device |
| CN108437198A (en) * | 2018-05-17 | 2018-08-24 | 眉县盛力机械制造有限公司 | High-efficient energy-saving environment friendly disappears grey mixer |
| CN113975948A (en) * | 2021-11-01 | 2022-01-28 | 山东首丰智能环保装备有限公司 | Dry desulfurization system |
| CN114247281A (en) * | 2020-09-22 | 2022-03-29 | 宝山钢铁股份有限公司 | Method for cooperatively treating desulfurized ash by wet desulfurization system |
| WO2022083455A1 (en) * | 2020-10-20 | 2022-04-28 | 威海市正大环保设备股份有限公司 | Integrated method and device for circulating semi-dry desulfurization and dust removal with humidification outside tower |
-
2006
- 2006-12-01 CN CN 200620048392 patent/CN200980986Y/en not_active Expired - Lifetime
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100460047C (en) * | 2006-12-01 | 2009-02-11 | 沙晓农 | Circulation fluidized bed dry method flue gas desulfur device |
| CN102266718A (en) * | 2010-06-07 | 2011-12-07 | 中国科学院过程工程研究所 | Semi dry process flue gas desulfurization method of circulating fluidized bed based on circulation, and apparatus thereof |
| CN102266718B (en) * | 2010-06-07 | 2014-07-30 | 中国科学院过程工程研究所 | Semi dry process flue gas desulfurization method of circulating fluidized bed based on circulation, and apparatus thereof |
| CN102397729A (en) * | 2011-12-12 | 2012-04-04 | 中联重科股份有限公司 | Dust removal case and have dust pelletizing system of this dust removal case |
| CN102397729B (en) * | 2011-12-12 | 2014-11-26 | 长沙中联重科环卫机械有限公司 | Dust removing box and dust removing system with same |
| CN107570000B (en) * | 2017-10-31 | 2024-06-21 | 苏州市淳然环境技术有限公司 | Deacidifying and dust removing device |
| CN107570000A (en) * | 2017-10-31 | 2018-01-12 | 苏州顺为环境科技有限公司 | Deacidifying dedusting device |
| CN108437198A (en) * | 2018-05-17 | 2018-08-24 | 眉县盛力机械制造有限公司 | High-efficient energy-saving environment friendly disappears grey mixer |
| CN108437198B (en) * | 2018-05-17 | 2024-01-30 | 眉县盛力机械制造有限公司 | High-efficiency energy-saving environment-friendly ash-removing mixer |
| CN114247281A (en) * | 2020-09-22 | 2022-03-29 | 宝山钢铁股份有限公司 | Method for cooperatively treating desulfurized ash by wet desulfurization system |
| WO2022083455A1 (en) * | 2020-10-20 | 2022-04-28 | 威海市正大环保设备股份有限公司 | Integrated method and device for circulating semi-dry desulfurization and dust removal with humidification outside tower |
| CN113975948B (en) * | 2021-11-01 | 2024-06-14 | 山东首丰智能环保装备有限公司 | Dry desulfurization system |
| CN113975948A (en) * | 2021-11-01 | 2022-01-28 | 山东首丰智能环保装备有限公司 | Dry desulfurization system |
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